GB2098666A - Generation of energy by means of a working fluid and regeneration of a working fluid - Google Patents
Generation of energy by means of a working fluid and regeneration of a working fluid Download PDFInfo
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- GB2098666A GB2098666A GB8114927A GB8114927A GB2098666A GB 2098666 A GB2098666 A GB 2098666A GB 8114927 A GB8114927 A GB 8114927A GB 8114927 A GB8114927 A GB 8114927A GB 2098666 A GB2098666 A GB 2098666A
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- working fluid
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- solvent solution
- regeneration
- regenerated
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F03—MACHINES OR ENGINES FOR LIQUIDS; WIND, SPRING, OR WEIGHT MOTORS; PRODUCING MECHANICAL POWER OR A REACTIVE PROPULSIVE THRUST, NOT OTHERWISE PROVIDED FOR
- F03G—SPRING, WEIGHT, INERTIA OR LIKE MOTORS; MECHANICAL-POWER PRODUCING DEVICES OR MECHANISMS, NOT OTHERWISE PROVIDED FOR OR USING ENERGY SOURCES NOT OTHERWISE PROVIDED FOR
- F03G7/00—Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for
- F03G7/04—Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for using pressure differences or thermal differences occurring in nature
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/06—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using mixtures of different fluids
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/06—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using mixtures of different fluids
- F01K25/065—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using mixtures of different fluids with an absorption fluid remaining at least partly in the liquid state, e.g. water for ammonia
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Abstract
A gaseous working fluid is expanded from a charged high pressure level to a spent low pressure level to release energy and the working fluid is regenerated by, in at least one regeneration stage, condensing the working fluid in an absorption stage (A) by dissolving it in a solvent solution while cooling with a cooling medium, the solvent solution comprising a solvent having an initial working liquid concentration which is sufficient to provide a solvent solution boiling range suitable for absorption of the working fluid; increasing the pressure of the solvent solution containing the dissolved working fluid by means of a pump (P) and evaporating the working fluid being regenerated by heating in an evaporation stage (E); withdrawing the evaporated working fluid for expansion in turbine 52 to release energy; and recycling the balance of the solvent solution remaining after evaporation of the working fluid, to constitute the solvent solution for the absorption stage of that regeneration stage. The preferred working fluid is ammonia, the solvent is water and the heat source is ocean thermal energy. <IMAGE>
Description
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GB 2 098 666 A 1
SPECIFICATION
Generation of energy by means of a working fluid, and regeneration of a working fluid
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This invention relates to the generation of energy by means of a working fluid, and to the regeneration of a working fluid. More particularly, this invention relates to a method of and to apparatus for generat-10 ing energy by means of a working fluid and for regenerating such a working fluid.
In the generation of energy by expansion of a working fluid, the energy which can be produced by expansion of the working fluid is limited by the 15 temperatures at which heating and cooling mediums can economically be provided for regeneration of the working fluid. The result is, therefore, that such a working fluid is expanded from a high pressure charged level to a low pressure spent level, with the 20 high pressure charged level being governed by the maximum pressure at which the working fluid can be evaporated with the available heating medium, and with the spent low pressure level being governed by the minimum pressure at which the work-25 ing fluid can be condensed with the available cooling medium.
In practice, therefore, expansion of the working fluid is controlled to provide a spent low pressure level at which the condensation temperature of the 30 working fluid is greater than the temperature of the cooling medium, to permit condensation of the working fluid.
In addition, in practice, regeneration is based on condensation of working fluid in a condenser 35 wherein the working fluid is arranged to flow in heat exchange relationship with an available cooling medium. Because of the desire to achieve maximum expansion of the working fluid, regeneration of working fluid is often effected where the tempera-40 ture difference between the condensation temperature of the spent working fluid at the spent level and the temperature of the available cooling medium is marginal-often as low as 1°C. This of necessity imposes a requirement for a large condenser with an 45 extensive heat exchange surface, and for a large supply of cooling medium, thereby substantially adding to the operating costs.
This is particularly significant where severe restraints are imposed by the temperatures of avail-50 able heating and cooling mediums as in the case of ocean thermal energy conversion systems.
In accordance with one aspect of the invention, there is provided a method of generating energy, which comprises expanding a gaseous working fluid 55 from a charged high pressure level to a spent low pressure level to release energy, and regenerating the spent working fluid by, in at least one regeneration stage:
(a) condensing the working fluid in an absorption 60 stage by dissolving it in a solvent solution while cooling with a cooling medium, the solvent solution comprising a solvent having an initial working fluid concentration which is sufficient to provide a solvent solution boiling 65 range suitable for absorption of the working fluid;
(b) increasing the pressure of the solvent solution containing the dissolved working fluid and evaporating the working fluid being regener-
70 ated by heating in an evaporation stage;
(c) withdrawing the evaporated working fluid for re-expansion to release energy; and
(d) recycling the balance of the solvent solution remaining after evaporation of the working
75 fluid, to constitute the solvent solution for the absorption stage of that regeneration stage.
In accordance with a further aspect of the invention there is provided a method of optimizing, within limits imposed by available sources of cooling and 80 heating mediums, the energy supply capability of a gaseous working fluid which is expanded from a charged high pressure level to a spent low pressure level to provide available energy, the method comprising expanding the gaseous working fluid to a 85 spent low pressure level, and regenerating the spent working fluid by, in at least one regeneration stage:
(a) condensing the working fluid being regenerated in an absorption stage by dissolving it in a solvent solution while cooling with the cooling 90 medium, the solvent solution comprising a solvent having an initial working fluid concentration which is sufficient to provide a solvent solution boiling range suitable for absorption of the working fluid;
95 (b) increasing the pressure of the solvent solution containing the dissolved working fluid, and evaporating the working fluid being regenerated by heating in an evaporation stage with the available heating medium; 100 (c) withdrawing the evaporated working fluid to constitute a charged working fluid; and
(d) recycling the balance of the solvent solution remaining after evaporation of the working fluid being regenerated, to constitute the sol-105 vent solution for the absorption stage of that regeneration stage.
In an embodiment of the invention the spent working fluid may be regenerated in a plurality of successive regeneration stages by increasing the pressure 110 in each stage until the working fluid has been regenerated to its charged state in the final regeneration stage.
The spent working fluid may thus be regenerated by feeding it to a first regeneration stage, feeding the 115 evaporated working fluid from each regeneration stage to a succeeding regeneration stage for further regeneration, and recycling within each regeneration stage the solvent solution remaining after evaporation of the working fluid in the evaporation stage 120 of that regeneration stage for the recycled solvent solution to constitute the solvent the solvent solution forthe absorption stage of that regeneration stage.
The working fluid may be expanded to a spent low 125 pressure level where the condensation temperature of the gaseous working fluid is below the minimum temperature of the cooling medium in the absorption stage.
Further in accordance with the invention, there is 130 provided a method of optimizing, within limits
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imposed by available sources of cooling and heating mediums, the energy supply capability of a gaseous working fluid which is expanded from a charged high pressure level to a spent low pressure level to 5 provide available energy, the method comprising expanding the gaseous working fluid to a spent low pressure level, and regenerating the spent working fluid by, in a plurality of successive regeneration stages, condensing the working fluid and then 10 evaporating the working fluid at an increased pressure, the working fluid being condensed in each regeneration stage by absorbing or dissolving it in a solvent solution while cooling with the cooling medium, the solvent solution comprising a solvent 15 having, in each stage, an initial working fluid concentration which is sufficient to provide a solvent solution boiling range suitable for absorption of the working fluid, and the working fluid being evaporated in each stage by increasing the pressure to a 20 level where the working fluid being regenerated can be evaporated with the available heating medium, and then evaporating the working fluid.
The invention further extends to apparatus for generating energy, the apparatus comprising 25 expansion means for expanding a gaseous working fluid from a charged high pressure level to a spent low pressure level to release energy, and a plurality of successive regeneration stages for regenerating such a spent working fluid, each regeneration stage 30 comprising:
(a) an absorber for receiving both a spent working fluid and a solvent solution for dissolving or absorbing the spent working fluid, the absorber having cirulation means for circulat-
35 ing a cooling medium through it to cool it;
(b) a pump for pumping a resultant solvent solution from the absorber to increase its pressure;
(c) an evaporator for receiving a resultant solvent 40 solution from the pump, the evaporator having circulation means for circulating a heating medium through it to heat it to evaporate such a working fluid to be regenerated;
(d) a separator for separating such an evaporated 45 working fluid being regenerated, from such a solvent solution;
(e) feed means to feed such an evaporated working fluid to the absorber of a succeeding regeneration stage;
50 (f) recycle means for recycling a solvent solution from the separator to the condenser;
and a feed conduit for feeding a regenerated working fluid from the separator of a final regeneration stage to the expansion means.
55 Since the solvent solution in each regeneration stage is recycled, the solvent solution constitutes a closed loop in that stage, and is separate from the solvent solution in each other regeneration stage. Furthermore, in each regeneration stage, the quan-60 tity of working fluid being regenerated is dissolved in the solvent solution of that stage, and the equivalent quantity of working fluid being regenerated is evaporated from the solvent solution in the evaporation stage of each regeneration stage.
65 It will be appreciated thatthe quantity of solvent solution, and the initial concentration of working fluid in the solvent solution in each regeneration stage will be separately adjusted as may be required for specific operating conditions, and as may be required for variations in the minimum temperature level of an available cooling medium.
The solvent of the solvent solution may be any suitable solvent which is a solvent for the working fluid, which has a boiling point above the maximum temperature which will be attained in any evaporation stage, and which will provide a solvent solution when working fluid is dissolved therein, which has a boiling point which decreases as the concentration of working fluid increases.
While the solvent solution is preferably a binary solution, it will be appreciated that it may be a solution of a plurality of liquids.
A number of working fluids which would be suitable, are known to those skilled in the art. Any of such working fluids may be employed in this invention.
In one embodiment of the invention, the working fluid and solvent may be in the form of hydrocarbons having appropriate boiling points. Thus, for example, the solvent may be in the form of butane or pentane while the working fluid may be in the form of propane. In an alternative example, the working fluid may be an appropriate freon compound, with the solvent being an appropriate solvent for that compound.
In a preferred embodiment of the invention, the working fluid is in the form of ammonia and the solvent is in the form of water, in this embodiment of the invention, at a pressure of one atmosphere the boiling point of water is 100°C whereas the boiling point of pure ammonia is -33°C. As the concentration of ammonia in water increases, the boiling point of the aqueous ammonia solution will decrease. From binary phase diagrams of water and ammonia solutions, the appropriate initial concentration of ammonia in the solvent solution for each regeneration stage, can readily be determined for this invention from the pressure and temperature which will prevail in each condensation stage.
In a preferred embodiment of the invention, the initial concentration of working fluid in the solvent solution in each regeneration stage, and the proportion of solvent solution to working fluid to be regenerated will be selected so that after complete absorption of the working fluid being regenerated in the absorption stage of that regeneration stage, the solvent solution will have a boiling point marginally above the minimum temperature attained in that absorption stage during use.
In practice, therefore, the minimum quantity of solvent solution will be employed which will satisfy this requirement thereby reducing cooling medium requirements to the minimum, and thereby further reducing heating medium requirements to the minimum.
It will be appreciated that since the pressure is increased between the absorption stage and evaporation stage of each regeneration stage, there will be a step-wise or incremental increase in pressure between each preceeding regeneration stage and
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each succeeding regeneration stage. It follows, therefore, that the initial concentration of working fluid in the solvent solution for each successive regeneration stage will be correspondingly higher to 5 provide a boiling range forthe solvent solution in each stage which is suitable for dissolving or absorbing the working fluid at the pressure prevailing in that stage.
In a preferred embodiment of the invention, the 10 pressure is increased between the absorption and evaporation stages of each regeneration stage, to the maximum pressure at which the working fluid being regenerated can be evaporated effectively in the evaporation stage by the, or by a heating 15 medium, available for heating the evaporation stage.
The pressure is, therefore, preferably increased in each regeneration stage to the maximum level where the solvent solution in each evaporation stage will, after evaporation of the working fluid in that 20 stage, have a boiling point marginally below the maximum temperature attainable in that evaporation stage.
By appropriate control of the pressure, evaporation of the required quantity of working fluid being 25 regenerated can be readily effected in each evaporation stage. Control valve means may, however, be provided to control the quantity of evaporated working fluid which is fed from each regeneration stage to each succeeding regeneration stage. Thus, if a 30 greater quantity of working fluid than that required for regeneration has been evaporated in an evaporator stage, onlythe required quantity will pass to the succeeding regeneration stage. The balance will be recycled with the solvent solution. 35 The method of this invention may preferably include the step of, in each regeneration stage, feeding the solvent solution and evaporated working fluid from the evaporation stage to a separation stage for separating the working fluid being regen-40 erated.
The separator stage may be provided by a separator of any conventional suitable type known to those skilled in the art.
The solvent solution which is recycled to the 45 absorption stage in each regeneration stage, is conveniently expanded to reduce its pressure to a pressure corresponding with or approaching that of the pressure of the working fluid being regenerated in that absorption stage.
50 In a preferred embodiment of the invention, in each regeneration stage, the solvent solution which is recycled, is recycled in heat exchange relationship with the evaporation stage to thereby reduce the heating medium requirements forthe evaporation 55 stage.
The solvent solution which is recycled in each regeneration stage, may be recycled at least partially in heat exchange relationship with the absorption stage.
60 Where the recycled solvent solution is recycled in heat exchange relationship with an absorption stage, the cooling medium requirement will decrease because the quantity of heat to be removed will remain constant, but the capacity of the absorp-65 tion stage will have to be increased. Conversely, if the recycled solvent solution is not recycled in heat exchange relationship with the absorption stage, the capacity of the absorption stage will decrease while the requirement of cooling medium will increase.
In practice, therefore, depending upon the source and availability of the cooling medium, on the basis of economic considerations, the reduced cost of supplying lesser quantities of cooling medium can be balanced against the capital costs of increasing the capacity of the absorption stages to determine whetherthe recycled solvent solution should be recycled in heat exchange relationship, or at least partially in heat exchange relationship with the absorption stages, or not at all.
In an embodiment of the invention, all of the absorption stages of the regeneration stages may be carried out separately in a single composite absorption stage which is cooled by means of cooling medium from a common source. Furthermore, all of the evaporation stages may be carried out separately in a single composite evaporation stage which is heated by means of a heating medium from a common source.
The apparatus of this invention may, therefore, include a single composite absorption unit and a single composite evaporation unit, with all the absorbers of the various regeneration stages being incorporated in the absorption unit, and all the evaporators of the various regeneration stages being incorporated in the evaporated unit.
While this invention may have various applications, and while various types of cooling and heating means known to those skilled in the art, may be employed, this invention can have particular application in regard to the utilization of readily and economically available cooling and heating mediums for the generation of energy.
The invention can, therefore, have specific application where lowtemperature differential heating and cooling mediums are employed.
A preferred application of the invention would, therefore, be in the field of thermal energy conversion using cool water withdrawn from a body of water as the cooling medium, and using, as heating medium, hot water from a body of water, water heated by solar heating, hot water heated additionally by solar heating means, or water or heating fluid in the form of waste heat fluids from industrial plants.
A preferred application of the invention would, therefore, be in the field of ocean thermal energy conversion [OTEC] where ocean surface water is used as the heating medium and ocean water withdrawn from a sufficient depth from an ocean is used as the cooling medium, thereby resulting in a low temperature differential between the heating and cooling mediums.
Normally, ocean water would be withdrawn from a depth of about 200 feet to provide the most economical cooling medium atthe lowest temperature. The temperature does not tend to decrease significantly beyond a depth of about 200 feet.
A further preferred application of the invention would be in regard to solar ponds for supplying the heating medium, and also the cooling medium if
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desired.
The invention further extends to a method of increasing the pressure of a gaseous working fluid from an initial low pressure level to a high pressure 5 level utilizing an available heating medium and utilizing an available cooling medium, which comprises incrementally increasing the pressure of the working fluid by, in a plurality of successive incremental regeneration stages:
10 (a) absorbing the working fluid being regenerated in an absorption stage by dissolving it in a solvent solution while cooling with such an available cooling medium; the solvent solution comprising a solvent having an initial working 15 fluid concentration which is sufficient to provide a solvent solution boiling range suitable for absorption of the working fluid;
(b) increasing the pressure of the solvent solution containing the dissolved working fluid, and
20 evaporating the working fluid being regenerated in an evaporation stage by heating with such an available heating medium;
(c) feeding the evaporated working fluid which is at an increased pressure level, to a succeed-
25 ing regeneration stage for absorp tion;
(d) recycling the balance of the solvent solution remaining after evaporation of the working fluid being regenerated, to constitute the sol-
30 vent solution forthe absorption stage of that regeneration stage; and
(e) withdrawing regenerated working fluid from a final regeneration stage.
The expansion of the working fluid from a charged 35 high pressure level to a spent low pressure level to release energy may be effected by any suitable conventional means known to those skilled in the art, and the energy so released may be stored or utilized in accordance with any of a number of conventional 40 methods known to those skilled in the art.
In a preferred embodiment of the invention, the working fluid may be expanded to drive a turbine of conventional type.
In an embodiment of the invention, where the 45 mass ratio between the solvent solution being recycled through an absorption stage and the working fluid being regenerated is sufficient, the pressure of the solvent solution leaving the evaporation stage may be utilized to increase the pressure of the work-50 ing fluid being regenerated which is introduced into the absorption stage with the recycled solvent solution.
In this embodiment of the invention, instead of expanding the solvent solution which is recycled to 55 reduce its pressure to a pressure corresponding with or approaching that of the pressure of the working fluid being regenerated in an absorption stage, the solvent solution may be injected into the absorption stage in such a manner as to entrain the working 60 fluid and drawthe working fluid into the absorption stage.
Various injection systems are known to those skilled in the art which could be used for this purpose. As an example, an injection system such as an injec-65 tion nozzle having a restricted zone to create a zone of low pressure may be used. With such an injection nozzle, the working fluid will be introduced into the proximity of the restricted zone so that the reduced pressure created will permit the working fluid to be introduced into the absorption stage.
It will be appreciated that, depending upon relative flow rates and pressures, it may still be necessary to control the pressure of the recycled solvent solution by expanding it to provide an appropriate pressure.
By utilizing the pressure, or at least part of the pressure, of the solvent solution which is recycled, this will contribute to an increase in pressure in the absorption stage. This can provide the advantage of improving absorption in the absorption stage, or can be utilized to permit expansion of the working fluid to an even lower spent level. In this event, the initial increase in pressure provided by the solvent solution may be utilized to increase the pressure in the absorption stage, to a level where absorption can be effectively achieved in accordance with this invention.
Applicant believes that this application of the pressure of the solvent solution will tend to be valuable in the first stage, and probably the first and second stages of a multi-stage regeneration system while, in a single stage system or a system employing only two stages it will tend to be less valuable. This will primarily be due to the fact that the mass ratio between the recycled solvent solution and the working fluid will not be sufficient.
Preferred embodiments of the invention are now described by way of example with reference to the accompany drawings.
Inthedrawings:-
Figure 1 shows a schematic representation of one embodiment of the method and apparatus of this invention;
Figure 2 shows a fragmentary schematic representation of the method and apparatus of Figure 1 incorporating a modification to the expansion stage;
Figure 3 shows a fragmentary schematic representation of a further embodiment of the invention in which injection means is utilized to inject the working fluid being regenerated;
Figure 4 shows a schematic representation of a further embodiment of the method and apparatus of this invention.
With reference to Figure 1 of the drawings, numeral 50 refers generally to apparatus for use in generating energy by the expansion of a gaseous working fluid from a charged high pressure level to a spent low pressure level to release energy, and for regenerating the spent working fluid.
The apparatus 50 includes expansion means in the form of a turbine 52 in which a gaseous working fluid is expanded from a charged high pressure level to a spent low pressure level to released energy to drive the turbine 52. The gaseous working fluid at the high pressure level is fed to the turbine 52 along charged line 54 and is discharged from the turbine 52 along spent line 56.
The apparatus 50 further includes regeneration means for regenerating the spent gaseous fluid. The regeneration means comprises four successive incremental regeneration stages.
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For ease of reference the components of each regeneration stage have been identified by a letter followed by a suffix in arabic numerals indicating the particular regeneration stage. In addition, the flow 5 lines for each regeneration stage have been identified by reference numerals having a prefix corresponding to that of the particular regeneration stage.
The first regeneration stage comprises an absorber A1 for condensing the gaseous working 10 fluid by dissolving it in a solvent solution, a pump P1 for pumping the solvent solution containing the dissolved working fluid to increase the pressure, evaporator E1 for evaporating the working fluid, and a separator SI for separating the evaporated work-15 ing fluid from the solvent solution.
The first regeneration stage includes an influent line 1-1 into which the spent gaseous working fluid from the spent line 56 and solvent solution from a solvent solution recycle line 1-13 are fed into the first 20 stage and through the absorber A1.
The resultant solvent solution from the absorber A1 is fed along line 1 -2 to the inlet of the pump P1. The solution is discharged from the pump P1 at an increased pressure along line 1-3 and through the 25 evaporator E1. The solvent solution and evaporated working fluid are fed from the evaporator E1 along line 1 -4 to the separator S1. The separated evaporated working fluid is fed from the separators1 along line 1 -5 to the influent line 2-1 of the second 30 stage. The solvent solution from the separator S1 is recycled along solvent solution recycle line 1-13 to the influent line 1-1.
The second, third and fourth regeneration stages correspond exactly with the first regeneration stage 35 except that the evaporated, separated working fluid from the separator S4 is withdrawn along line 4-5 and fed into the charged line 54 to repeat the cycle.
In the preferred embodiment of the invention, the gaseous working fluid is ammonia, whereas the sol-40 vent is water. In addition, in the preferred embodiment of the invention, the apparatus 50 is an apparatus for use in producing energy by ocean thermal energy conversion.
The apparatus 50 is, therefore, conveniently instal-45 led on the seashore or on a floating platform. In addition, the apparatus 50 includes pump means [not shown] for pumping surface water from the surface of an ocean to the evaporators of the apparatus to constitute the heating medium forthe apparatus, 50 and includes pump means [not shown] for pumping cold water from a sufficient depth of such an ocean for constituting the cooling medium for cooling the absorbers of the apparatus 50.
Thus, the absorber A1 includes circulation means 55 having an inlet 1-9 and an outlet 1-10 for circulating deep ocean water through the absorber A1. Similarly, the evaporator E1 includes an inlet 1-11 and an outlet 1-12 for circulating ocean surface water through the evaporator for heating the evaporator 60 E1.
Further, in each regeneration stage, the recycle line 1-13,2-13,3-13 and 4-13 has an evaporator heat exchange line 1 -15,2-15,3-15 and 4-15, respectively, passing in heat exchange relationship through the 65 evaporator E.
In addition, in each of the regeneration stages, the solvent solution recycle line -13 may have a condenser heat exchange I ine 1 -16,2-16,3-16 and 4-16, respectively, extending in heat exchange relation-70 ship through the absorber A or, alternatively, may completely bypass the absorber A as indicated by chain-dotted lines 1-18,2-18,3-18 and 4-18.
Where the recycled solvent solution passes in heat exchange relationship through the absorber of each 75 regeneration stage, it will assist in cooling the absorber and will thus reduce the quantity of cooling water required to effectthe required cooling in that absorber since the quantity of heat to be transferred will remain constant. It will, however, necessitate an 80 increase in the absorber capacity and thus, in the absorber size.
In practice, therefore, the capital cost of an increase in absorber size can be balanced against the cost of the additional quantity of cooling medium to 85 decide, on the basis of pure economics, as to whetherthe recycle line should pass through the absorbers, should completely bypass the absorbers, or should pass partially through the absorbers.
In the preferred embodiment of the invention, the 90 recycle lines will bypass the absorbers.
In the preferred embodiment of the invention, the gaseous working fluid is ammonia, whereas the solvent solution is a solution of ammonia in water.
The use of the apparatus 50, and thus the process 95 of this invention, is now described with reference to a preferred ocean thermal energy conversion system typically employing, as heating medium, surface water at a temperature of 27°C, and employing as cooling medium, deep ocean water [typically at a 100 depth of not less than about 200 feet| having a temperature of about 4°C.
Since the boiling point of pure ammonia is —33°C at a pressure of one atmosphere, and since the minimum temperature of the cold water cooling 105 medium is4°C, it would normally not be possible to regenerate ammonia at a pressure of one atmosphere by using such a cooling medium. In other words, regeneration would only be possible if the ammonia working fluid were at a pressure where the 110 boiling point of ammonia is above 4°C.
In other words, regeneration of the gaseous working fluid would only be possible if the working fluid is expanded across the turbine 52 to a pressure at which it is capable of regeneration with the available 115 cooling medium. This imposes a direct and severe limitation on the energy which can be generated since the maximum pressure to which the ammonia working fluid can be regenerated is also limited by the evaporation capacity of the hot water heating 120 medium at27°C.
In practice, utilizing surface water at a temperature of about 27°C, evaporation of ammonia in the final evaporator E4 can only be achieved in an effective manner at a maximum pressure of about nine 125 atmospheres.
It will be appreciated, therefore, that if the working fluid can be expanded from a charged level of nine atmospheres to a spent level pressure of one atmosphere, as opposed to a spent level pressure of say 130 only fou r atmospheres, the quantity of energy
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released will be increased substantially.
In the preferred process as illustrated in Figure 1, the gaseous ammonia working fluid is indeed allowed to expand across the turbine 52 from a pres-5 sure of about nine atmospheres to a pressure of about one atmosphere.
A specific quantity of gaseous working fluid to be regenerated, at a spent pressure level of one atmosphere is, therefore fed to the first stage along 10 influent line 1-1.
This quantity of gaseous working fluid is condensed in the absorber A1 by dissolving it in a solvent solution which is fed along solvent solution recycle line 1-13 into the influent line 1-1 atthe same 15 pressure of one atmosphere.
In the preferred embodiment of the invention, the solvent solutions will not be passed in heat exchange relationship through the absorbers. Thus, the spent gaseous ammonia, which may contain 20 about 10% by weight of liquid ammonia, will be at a temperature of about -33°C, whereas the corresponding solvent solution will be at a temperature of about 8°C.
The solvent solution comprises water having an 25 initial ammonia concentration which is sufficient to provide a binary solution which atthe pressure of one atmosphere, has a boiling point within the temperature range which will prevail in the absorber A1. Further, the proportion of solvent solution to the 30 quantity of working fluid to be regenerated is such that after the solvent solution has dissolved the quantity of working fluid to be regenerated in the absorber A1, the resultant binary solution will have a concentration which will provide, atthe pressure of 35 one atmosphere, a boiling point marginally above the minimum temperature of the cooling medium. The boiling point of the solvent solution will thus be in the region of about 6°C where the minimum temperature of the cold water is about 4°C. 40 In this way it will be insured that the total quantity of working fluid to be regenerated will dissolve in the solvent solution, and that the minimum quantity of solvent solution to dissolve that quantity of gaseous ammonia will be employed thereby reducing the 45 cold water requirements and the capacity of the absorber A1 to the practical minimum.
The solvent solution containing the dissolved working fluid being regenerated, will leave the absorber A1 at a temperature of about 6°C and at a 50 pressure of one atmosphere, and is pumped by the pump P1 to the evaporator E1.
The pump P1 is controlled to increase the pressure of the solvent solution to the maximum pressure at which the dissolved ammonia working fluid can be 55 effectively evaporated in the evaporator E1 by means of the surface water heating medium at a maximum temperature of 27°C.
Preferably, the pressure increase is controlled so that after evaporation of the quantity of working fluid 60 being regenerated, the solvent solution in the evaporator E1 will have a boiling point marginally below 27°C, such as about 25°C.
This pressure can readily be determined from a binary water/ammonia phase diagram in relation to 65 the prevailing ammonia concentration and temperature range in the evaporator E1.
It will naturally be appreciated that the initial concentration of ammonia in water for the solvent solution, as also the required quantity of solvent solu-70 tion; which is fed to the absorber A1, can also readily be determined from such a phase diagram on the basis of the known pressure and temperature range.
The evaporated working fluid and solvent solution are fed along line 1-4 to the separator S1, where they 75 are allowed to separate.
From the separator S1, the solvent solution, at a temperature of about 25°C will be recycled along the solvent solution recycle line 1-13 to constitute the solvent solution for the first stage. The separated, 80 evaporated ammonia working fluid at about 25°C is fed from the separator S1 to the second regeneration stage along influent line 2-1. As in the case of the first regeneration stage, the quantity of working fluid being regenerated, is mixed with a solvent solution 85 recycled from a separator S2 of the second regeneration stage along the solvent solution recycle line 2-13 for dissolving the working fluid in the absorber A2.
Since the pressure in the absorber A2 will be greater than the pressure in the absorber A1, it follows 90 that the initial concentration of ammonia in the solvent solution forthe second stage will be correspondingly higherto insure that an appropriate boiling point is again provided for effectively dissolving or absorbing the working fluid being regenerated in 95 the absorber A2.
It will be appreciated that the solvent solution which is recycled from the separator S to the absorber A in each stage leaves the separator S at a higher pressure than the pressure of the influent 100 working fluid. Each solvent solution recycle line 1-13, 2-13,3-13 and 4-13, therefore, includes a pressure-reducing valve V1, V2, V3 and V4, respectively, for reducing the pressure of the recycled solvent solution to the same pressure as that of the influent 105 working fluid being regenerated.
For each successive regeneration stage, therefore, the initial concentration of ammonia in the solvent solution will increase step-wise in correspondence with the step-wise increase in pressure provided by 110 the pump means in each stage.
It will be appreciated that the apparatus will include an appropriate number of regeneration stages until the quantity of working fluid being regenerated, has been regenerated to the appropri-115 ate charged high pressure level in a final regeneration stage such as the fourth regeneration stage shown in the drawing. It will further be appreciated that the spent pressure level to which the working fluid is expanded, will likewise determine the 120 number of regeneration stages required. Thus if the working fluid is expanded to only say 3 atmospheres, only two or three regeneration stages may be required.
In the embodiment illustrated in the drawing, the 125 pump means P4 will increase the pressure of the solvent solution to about nine atmospheres thereby yielding a charged regenerated working fluid at a pressure of about nine atmospheres which is withdrawn from the separator S4 and fed along the 130 charged line 54 to the turbine 52.
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It will be appreciated that in the preferred embodiment of the invention, the process will be carried out as a continuous process in which a constant quantity of working fluid by unittime is continuously 5 being expanded across the turbine 52 and is then continuously being regenerated in the regeneration means.
To further illustrate the use of the invention in the preferred embodiment as illustrated in Figure 1,typ-10 ical parameters of the process are now indicated with reference to specific theoretical calculations performed on the basis of 1 kilogram of gaseous ammonia working fluid, and on the basis of deep ocean water at a minimum temperature of 4°C as 15 cooling medium, and surface ocean water at a maximum temperature of 27°C as heating medium.
These parameters as calculated are set out in Tables I, II, III and IV below for the first, second, third and fourth regeneration stages, respectively. 20 In each table, the particular point at which the parameter has been calculated, is indicated by the appropriate reference numeral in the drawing. These points are listed in the first column of each table.
The columns in the tables are as follows: 25 (a) First column-reference numerals (RN);
(b) Second column -temperature (t) in °C;
(c) Third column - pressure (p) in atmospheres;
(d) Fourth column — ratio by weight of total ammonia (dissolved and 30 undissolved) to water plus total ammonia (RATIO);
(e) Fifth column —weight (w) in kilograms; and
(f) Sixth column - Enthalpy (E) in kcal/g.
TABLE I
RN
t
P
RATIO
w
E
1-0
-32.0
1.0
.9920
1.0000
354.45
1-1
+ 9.0
1.0
.4266
22.2556
-642
1-2
- 6.0
1.0
.4266
22.2556
- 20.0
1-3
+ 6
1.8
.4266
22.2556
- 20.0
1-4
+25.0
1.8
.4266
22.2556
17.9730
1-5
+25.0
1.8
.9920
1.0000
400.0
1-6
+25.0
1.8
.4000
21.2556
0.0
1-7
+ 8.0
1.8
.4000
21.2556
- 23.4
1-8
+ 8.0
1.0
.4000
21.2556
- 23.4
TABLEII
RN
t
P
RATIO
w
E
2-1
+10.0
1.8
.5160
17.2457
9.4125
2-2
+ 6.0
1.8
.5160
17.2457
-10.80
2-3
+ 6.0
3.0
.5160
17.2457
-10.80
2-4
+25.0
3.0
.5160
17.2457
28.6905
2-5
+25.0
3.0
.9920
1.0000
403.0
2-6
+25.0
3.0
.4867
16.2457
5.65
2-7
+ 8.0
3.0 '
.4867
16.2457
- 14.63
2-8
+ 8.0
1.8
.4867
16.2457
- 14.63
TABLE III
RN
t
P
RATIO
w
E
3-1
+ 10.0
3.0
.6490
8.0000
48.625
3-2
+ 6.0
3.0
.6490
8.0000
10.00
3-3
+ 6.0
5.0
.6490
8.0000
10.00
3-4
+25.0
5.0
.6490
8.0000
68.688
3-5
+25.0
5.0
.9920
1.0000
409.5
3-6
+25.0
5.0
.6000
7.0000
20.00
3-7
+ 8.0
5.0
.6000
7.0000
- 2.00
3-8
+ 8.0
3.0
.6000
7.0000
- 2.00
TABLE IV
RN
t
P
RATIO
w
E
4-1
+10.0
5.0
0.9000
5.4231
124.45
4-2
+ 6.0
5.0
0.9000
5.4231
80.0
4-3
+ 6.0
9.0
.9000
5.4231
80.0
4-4
+25.0
9.0
.9000
5.4231
139.59
4-5
+25.0
9.0
.9920
1.0000
412.0
4-6
+25.0
9.0
.8792
4.4231
78.0
4-7
+ 8.0
9.0
.8792
4.4231
60.0
4-8
+ 8.0
9.0
.8792
4.4231
60.0
4-9
+ 8.0
5.0
.8792
4.4231
60.0
From the above theoretical calculations, the total 35 heat supplied to the four evaporator stages amounted to 1258.35 kcals, while the total heat removed from the four absorption stages amounted to 1200.8 kcals.
The difference of 57.55 is the work putin per kilog-40 ram of working fluid regenerated and thus the theoretical amount of work which is available.
The energy required to operate the pumps was calculated to be 2.08 kcals/kg of working fluid regenerated.
45 The theoretical amount of work available is therefore 55.47 kcal/kg of working fluid.
If it is assumed that the efficiency of the turbine is 85%, the theoretical thermal efficiency will be 4.408%.
50 The theoretical thermal efficiency of an ideal Car-not cycle system operating with a cooling medium at a constant temperature of 4°C and with a heating medium at a constant temperature of 27°C, would be 7.04%. However, considering that the temperature of 55 the heating and cooling mediums must change in such a process, the efficiency of the theoretical ideal thermodynamical cycle will be only about 4.9%.
Therefore, the ratio of the efficiency of a system in accordance with this invention on the basis of the 60 theoretical calculations, would be:
(a) 62.55% in relation to an ideal Carnot cycle system;
(b) about 82% in relation to an ideal thermodynamical cycle under corresponding con-
65 ditions.
It is an advantage of the embodiment of the invention as illustrated with reference to the drawing, that an effective system can be provided for generating energy by using the relatively low temperature diffe
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rential between surface ocean water as heating medium and deep ocean water as cooling medium.
it is a further advantage of this embodiment that a system can be provided for regeneration of spent 5 gaseous ammonia at a relatively low level of about one atmosphere or less.
It is a further advantage of the embodiment of the invention as illustrated, that because the regeneration range of the gaseous working fluid has been 10 increased, the gaseous working fluid can be expanded from a high pressure level of about nine atmospheres, to a low pressure level of about one atmosphere or less. Thus, the quantity of energy available for release is substantially greater than 15 would be the case if the working fluid were expanded from a pressure of about nine atmospheres to a pressure of only about four or five atmospheres.
The embodiment of the invention as illustrated in 20 the drawing can provide a further advantage arising from the fact that the cold water requirements need only be sufficient to provide a final temperature in each absorber of about 6°C. The temperature of the cold water cooling medium can thus increase across 25 each absorber as indicated in the above tables. Thus, the cooling medium requirements will be substantially less than would be the case if it were necessary to supply a sufficient quantity of cooling water at a sufficient rate to approach the Carnot cycle ideal 30 where the cooling medium would remain at the constant minimum temperature. The same considerations apply to the heating medium, where the hot water is allowed to cool from about 27°C to the temperature indicated in the above tables across 35 each evaporator stage thereby again providing a substantially reduced heating water requirement over that required by the ideal Carnot cycle operation.
It will be appreciated that since, in each absorber, 40 the cooling range forthe solvent solution and working fluid is substantially the same, and the temperature range for the cooling medium is substantially the same, the absorbers of the four regeneration stages can conveniently be combined into a single 45 composite absorberthrough which the lines 1-1,2-1, 3-1 and 4-1 pass separately for cooling by means of a single circulating supply of cold water. In the same way, all the evaporators can be combined in a single composite evaporator heated by means of the cir-50 culating hotwaterfrom a single source.
It will further be appreciated that, theoretically, the quantity of solvent solution in each regeneration stage should remain constant, and that the initial concentration of ammonia in waterto constitute the 55 solvent solution, should also remain constant for constant minimum cooling watertemperatures and constant maximum heating watertemperatures.
In practice, however, the quantity of solvent solution will have to be adjusted during use to compen-60 sate for varying conditions and for losses. In addition, the concentration of ammonia in water in each regeneration stage, will have to be adjusted periodically in relation to seasonal variations in the minimum temperature of cold water and maximum 65 temperature of hot water.
It will also be appreciated that where heating of the hot water can economically be achieved, such as by solar heating orthe like, the effectiveness of the process of this invention can be improved. Such 70 supplemental heating will, therefore, be employed under appropriate conditions if dictated by economic considerations.
With reference to Figure 2 of the drawings, numeral 150 refers generally to an alternative embodi-75 ment of the method and apparatus of this invention to the embodiment illustrated in Figure 1.
The apparatus 150 corresponds substantially with the apparatus 50 and corresponding parts are indicated by corresponding reference numerals. 80 In the apparatus 150, in place of the single turbine 52 of the apparatus 50, a two-stage turbine system is employed comprising afirstturbine 152 and a second turbine 153.
The charged working fluid is partially expanded 85 across the first turbine 152 into a heat exchange vessel 170.
From the heat exchange vessel 170 the partially expanded working fluid is led along separate conduits 171 and 172 through the absorber A2 and 90 through the absorber A1 respectively in heat exchange relationship with the cooling water.
Thereafter the partially spent working fluid is further expanded across the second turbine 153 to its final spent level. It is then fed, as before, along the 95 spent line 56 to the influent line 1 -1.
Applicant believes that by utilizing a two-stage turbine system with heat exchange of the partially expanded working fluid, the effectiveness of the system can be improved particularly where the system 100 includes a number of regeneration stages. Applicant believes that it will tend to be less significant where fewer stages are employed.
With reference to Figure 3 of the drawings, the drawing shows, to an enlarged scale, the apparatus 105 of Figure 1 which has been adapted in the first and second regeneration stages forthe pressure of the recycled solvent solution to be utilized in increasing the pressure of the influent spent working fluid into the absorption stage A1 and the absorption stage A2 110 respectively.
As indicated in Figure 3, the absorption stage A1 incorporates an injection system for injecting the recycled solvent solution at a pressure substantially higher than the pressure of the spent working fluid 115 into the absorber A1.
The injection system is in the form of an injection nozzle 180 having an intermediate restricted zone to generate a zone of low pressure.
The spent line 56 joins the nozzle 180 atthe 120 restricted zone and, as is known those skilled in the art, in an attitude where the reduced pressure generated atthe restricted zone by the solvent solution being injected through the nozzle 180 into the absorber A1, will draw the spent working fluid into 125 the nozzle 180 and thus into the absorber A1.
It will be appreciated that the effectiveness of this system will depend upon the mass ratio between the solvent solution being recycled and the working fluid being regenerated.
130 Ifthe ratio is to low, itwill not be possible to intro
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GB 2 098 666 A
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duce the total quantity of working fluid being regenerated by means of the flow of the solvent solution being recycled.
In practice therefore, depending upon conditions, 5 it may be necessary to partially reduce the pressure of the solvent solution being recycled before entry into the nozzle 180, or it may be necessary to introduce some of the working fluid being regenerated through the nozzle 180, and the remainder directly 10 into the absorber A1.
While the absorber A2 has not been illustrated in Figures, it will be appreciated that the working fluid being regenerated in the second regeneration stage will be introduced into the absorber A2 by means of 15 an injection system corresponding to that of the absorber A1.
The embodiment of the invention as illustrated in Figure 3 of the drawings, can provide the advantage that the pressure of the solvent solution being recy-20 cled in the first and second stages respectively can be at least partially utilized to introduce the working fluid being regenerated, and to increase the pressure in the first and second absorbers A1 and A2.
This affect can be utilized to improve the effective-25 ness of absorption in the first and second absorbers A1 and A2. Alternatively, or in addition, this feature can be utilized to permit expansion of the charged working fluid to a yet lower pressure across the turbine 52, with reliance being placed on the pressure 30 contribution of the solvent solution being recycled to raise the pressure in the absorber A1 to a level where effective absorption of the working fluid being regenerated can be effected. Similarly, if employed in relation to the second regeneration stage, the 35 same considerations will apply where the working fluid introduced into the absorber A2 can be at a lower pressure, and reliance is placed on the pressure of the solvent solution being recycled into the absorber A2, to increase the pressure to a level for 40 effective absorption in the absorber A2.
Applicant believes that the injection system can be advantageous in the apparatus 50 particularly in the first and second stages, but would tend to have lesser value in subsequent stages.
45 With reference to Figure 4 of the drawings, reference numeral 450 refers generally to yet a further alternative embodiment of the method and apparatus of this invention.
The system 450 as illustrated in Figure 4, is 50 designed for use where the charged working fluid is expanded to a relatively higher level than the level described with reference to Figures 1 to 3, but regeneration of the spent working fluid is effected in accordance with this invention to provide an 55 economical system with high efficiency.
The apparatus450 includes a turbine 452, and absorber A, a pump P, a regenerator R, an evaporator E and a separator S.
The spent working fluid expanded across the tur-60 bine 452 is fed along spent line 456 to influent line 464. Solvent solution which is recycled from the separator S along solvent solution recycle line 465 is fed through a pressure reducing valve V to reduce the pressure of the solvent solution to that of the 65 spent working fluid, and then into the absorber A
through the influent line 464.
As described with reference to Figure 1, cooling medium in the form of cold deep ocean water is circulated in heat exchange relationship through the 70 absorber A by means of conduit 461, while heating surface water is circulated through evaporator E in heat exchange relationship therewith, along conduit 463.
The spent working fluid is absorbed by the solvent 75 solution in the absorber A whereafter the solvent solution containing the absorbed working fluid has its pressure increased by the pump P.
The solvent solution containing the absorbed working fluid is fed from the pump P along line 466 80 through the regenerator R and then to the evaporator E for evaporation of the dissolved working fluid being regenerated.
The solvent solution being recycled along the line 465, is passed in heat exchange relationship with the 85 solvent solution passed through the regenerator R to effect heat exchange.
From the evaporator E, the evaporated fluid being regenerated and the solvent solution passes to the separator S for separation, whereafter the separated 90 charged working fluid is fed along charged line 454 to the turbine 452.
To illustrate this embodiment of the invention, typical parameters of the process of the system of Figure 4, are now indicated with reference to specific 95 theroetical calculations performed on the basis of 1 kilogram of gaseous ammonia working fluid, and on the basis of deep ocean water at a minimum temperature of 4°C as cooling medium, and surface ocean water at a maximum temperature of 27°C as heating 100 medium.
These parameters as calculated are set out in Table V below. The particular point at which the parameter has been calculated, has been indicated by the appropriate reference numeral in Figure 4. 105 These points are listed in the first column of Table V.
10
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TABLE V
POINTS TEMPERATURE PRESSURE CONCENTRATION MASS ENTHALPY °C atm. Kg NHJKg Kg KCallKg
Solution
0
+25
5.5
0.9920
1.00
388.0
1
+12
5.5
0.9368
1.75
248.78
2
+ 8
5.5
0.9368
1.75
75.00
3
+ 8
9.0
0.9368
1.75
75.00
4
+12
9.0
0.9368
1.75
80.64
5
+25
9.0
0.9368
1.75
265.45
6
+25
9.0
0.9920
1.00
407.30
7
+25
9.0
0.8632
0.75
76.32
8
+13
9.0
0.8632
0.75
63.16
9
+10
9.5
0.8632
0.75
63.16
Itwill be noted from Table V that the working fluid is expanded from a charged level of 9 atmospheres to a spent level of 5.5 atmospheres. It will further be noted thatthe spent working fluid and solvent solu-5 tion enter the absorber A at a temperature of 12°C, and thatthe solvent solution containing the absorbed working fluid being regenerated, leaves the absorber A at a temperature of about 8°C.
By using an absorber A for absorbing the spent 10 ammonia working fluid, and by having an appropriate initial concentration of ammonia in water for the solvent solution being recycled, absorption of the ammonia working fluid can commence in the absorber A at a temperature of 12°C or slightly 15 higher, and complete absorption will have occurred by the time the temperature has been reduced to about 8°C by the cooling medium at4°C.
There is therefore a significanttemperature difference between the temperature of the cooling 20 medium and the minimum temperature required for complete absorption of the working fluid being regenerated.
In contrast with a system employing a conventional condensation stage forthe condensation of a 25 working fluid such as ammonia, condensation of gaseous ammonia at 5.5 atmospheres would only commence at a temperature of about 5°C resulting in a marginal difference of 1°C between the temperature of condensation and the temperature of the 30 available cooling medium, which is at4°C.
Thus, before condensation can occur in a condensation stage, the temperature of the working fluid would have to be reduced to about 5°C by the cooling medium at4°C. Itwill be appreciated that 35 because ofthe marginal temperature difference, the requirements of cooling waterwill be substantial and a substantial heattransfer surface will be required.
In contrast therewith, by utilizing an absorber in 40 accordance with this invention, while both the working fluid being regenerated and the solvent solution being recycled will have to be cooled, because absorption of working fluid can commence at a temperature substantially above the temperature of 45 the cooling medium, and can be completed at a temperature substantially above the temperature of the cooling medium, the amount of cooling water required can be reduced substantially and/orthe heattransfer surface requirement can be reduced 50 substantially.
In practice, on the basis of economics, the cooling water requirements, the heattransfer surface area, and the temperature difference between the temperature ofthe cooling water and the temperature 55 required for complete absorption ofthe spent working fluid, can be balanced to achieve the most economical system in the light ofthe operating parameters and capital costs.
Because the solvent solution containing the work-60 ing fluid being regenerated would leave the absorber A at a temperature higher than the temperature of a condensed working fluid leaving a condenser, evaporation in the evaporator E will be facilitated. By additionally circulating the solvent solution 65 being recycled and the solvent solution containing the absorbed working fluid in heat exchange relationship through the regenerator R, both absorption in the absorber A and evaporation in the evaporator E will be improved.
70 The system 450 therefore provides the advantage of an increased enthalpy drop across the turbine 452 and provides a system of increased efficiency and economy.
To illustrate the advantages ofthe system in 75 accordance with this invention, calculations have been performed to compare the system illustrated in Figure 4 with a conventional OTEC system utilizing a conventional Rankine cycle under the same operating parameters imposed by the temperatures ofthe 80 heating and cooling mediums. The parameters for the Rankine cycle system were obtained from the publication entitled "OTEC Pilot Plan Heat Engine" by D. Richards and L. L. Perini, John Hopkins University, OTC3592,1979.
85 This comparison is set out in Table VI below.
11
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11
TABLE VI
COMPARISON OF OFF-DESIGN OPERATING CHARACTERISTICS OF OTEC PLANTS WITH AMMONIA CLOSED RANKINE CYCLE-\j\ AND WATER-AMMONIA ABSORB-TION CYCLE OF FIGURE 4 IN A CCORDANCE WITH THIS INVENTION - [.2]
RANKINE-[1]
FIGURE 4 CYCLE-[2]
Warm water temperature
°C
+27.89
+27.89
Cold water temperature
°C
+4.00
+4.00
Pressure of evaporation atm.
8.8516
9.0
Pressure of condensation atm.
6.2784
5.5
Inlet turbine temperature
°C
+20.389
+25.00
Outlet turbine temperature
°C
+ 10.00
+7.00
Expansion ratio kcai
1.41
1.636
Enthalpy drop through turbine
8.524
16.984
Turbine efficiency kg
0.88
0.88
Turbine-generator power
MW
13.76
12.452
Sea water pumps power
MW
2.856
1.832
Ammonia pump power
MW
0.408
0.124
Aux power
MW
0.151
0.151
Net electrical power
MW
10.345
10.345
Evaporator water flow kg/h
158.76 x10s
107.87 x10s
Condenser water flow kg/h
158.76 x106
95.86 x106
Ammonia flow through turbine kg/h
1.388 x10s
0.6304 x10s
Sea watertemperature drop
evaporator
°C
2.580
1.89
condenser/absorber
°c
2.505
2.0
TABLE VI CONTINUED
RANKINE-[1]
FIGURE 4 CYCLE-[2]
Heat flow through evaporator condenser/absorber regenerator kcal/h kcal/h kcal/h
409.583x106 397.752 x106 0.0
203.880 x106 191.715x10s
6.222 x10s
Average temperature difference in evaporator in condenser/absorber in regenerator
°C °C °C
6.12 4.635
4.056 4.933 9.87
Heat exchangers surface area evaporator condenser/absorber regenerator Total m2 m2 m2
78,272.5 100,953.65
0.0 179,681.15
59,136.79 45,722.09
990.87 105,849.75
Net thermal efficiency
%
2.1716
4.3627
Thermal efficiency ratio between [2] &[l] = 2.009 Cold water flow decrese in [2] % =39.62
Heat exchangers area decrase in [2] % =41.09
The significant advantages ofthe system of Figure 10 4 in relation to the conventional Rankine cycle system are clearly apparent from Table VI above. It is clearthatthe system in accordance with this invention can provide significant imporvements in efficiency and economy. This is particularly significant 15 in OTEC systems and related systems where the severe restraints imposed by the temperatures ofthe available heating and cooling mediums have heretofore presented a serious barrier to commercial utilization of OTEC systems.
Claims (1)
1. A method of generating energy, which comprises expanding a gaseous working fluid from a charged high pressure level to a spent low pressure level to release energy, and regenerating the spent working fluid by, in at least one regeneration stage:
(a) condensing the working fluid in an absorption
12
GB 2 098 666 A
12
stage by dissolving it in a solvent solution while cooling with a cooling medium, the solvent solution comprising a solvent having an initial working fluid concentration which is suf-5 ficientto provide a solvent solution boiling range suitable for absorption ofthe working fluid;
(b) increasing the pressure ofthe solvent solution containing the dissolved working fluid and
10 evaporating the working fluid being regenerated by heating in an evaporation stage;
(c) withdrawing the evaporated working fluid for re-expansion to release energy; and
(d) recycling the balance ofthe solvent solution 15 remaining after evaporation ofthe working fluid, to constitute the solvent solution forthe absorption stage of that regeneration stage.
2. A method according to claim 1, in which the spent working fluid is regenerated in a plurality of
20 successive regeneration stages by feeding the spent working fluid to a first regeneration stage, feeding the evaporated working fluid for each regeneration stage to a succeeding regeneration stage for further regeneration, withdrawing regenerated charged 25 working fluid from the final regeneration stage for re-expansion to release energy, and recycling within each regeneration stage the solvent solution remaining after evaporation ofthe working fluid in the evaporation stage of that regeneration stage forthe 30 recycled solvent solution to constitute the solvent solution forthe absorption stage of that regeneration stage.
3. A method according to claim 1 or claim 2, in which the working fluid is expanded to a spent low
35 pressure level at which the condensation temperature ofthe working fluid is belowthe minimum temperature ofthe cooling medium.
4. A method according to anyone of claims 1 to
3, in which, in each regeneration stage, the initial
40 concentration of working fluid in the solvent solution is sufficient, and the proportion of solvent solution to working fluid to be regenerated is such that after absorption of the working fluid being regenerated in that absorption stage, the solvent solution will have 45 a boiling point marginally above the minimum temperature attained in that absorption stage.
5. A method according to any one of claims 1 to
4, in which the pressure is increased between the absorption and evaporation stages of each regenera-
50 tion stage to the maximum pressure at which the working fluid being regenerated in that stage can be evaporated from the solvent solution in the evaporation stage by a heating medium available for heating the evaporation stage, and in which, in each regen-55 eration stage, the solvent solution which is recycled to the absorption stage is expanded to reduce its pressure to the pressure ofthe working fluid being regenerated in that absorption stage.
6. A method according to any one of claims 1 to 60 5, in which, in each regeneration stage, the solvent solution and evaporated working fluid are fed from the evaporation stage to a separation stage for separating the working fluid being regenerated.
7. A method according to any one of claims 1 to 65 6, in which, in each regeneration stage, the solvent solution which is recycled is recycled at least partially in heat exchange relationship with the solvent solution containing the dissolved working fluid between the absorption and evaporation stages.
8. A method according to claim 2, in which all of the absorption stages ofthe successive regeneration stages are carried out separately in a single composite absorption stage which is cooled by means of the cooling medium, and in which all ofthe evaporation stages ofthe successive regeneration stages are carried out separately in a single composite evaporation stage.
9. A method according to any one of claims 1 to 8, in which the cooling medium is provided by cool water withdrawn from a body of water, and in which each evaporation stage is heated by means of hot water withdrawn from the same body of water.
10. A method according to claim 2, in which the working fluid being regenerated is introduced into each absorption stage at a pressure where the condensation temperature ofthe working fluid is below the minimum temperature ofthe cooling medium.
11. Apparatus for generating energy, the apparatus comprising expansion means for expanding a gaseous working fluid from a charged high pressure level to a spent low pressure level to release energy, and a plurality of successive regeneration stages for regenerating such a spent working fluid, each regeneration stage comprising:
(a) an absorber for receiving both a spent working fluid and a solvent solution for dissolving the spent working fluid, the absorber having circulation means for circulating a cooling medium through itto cool it;
(b) a pump for pumping a resultant solvent solution from the absorber to increase its pressure;
(c) an evaporatorfor receiving a resultant solvent solution from the pump, the evaporator having circulation means for circulating a heating medium through itto heat itto evaporate such a working fluid to be regenerated;
(d) a separator for separating such an evaporated working fluid being regenerated, from such a solvent solution;
(e) feed means to feed such an evaporated working fluid to the absorber of a succeeding regeneration stage;
(f) recycle means for recycling a solvent solution from the separator to the absorber; and
(g) a feed conduit for feeding a regenerated working fluid from the separator of a final regeneration stage to the expansion means.
12. A method of increasing the pressure of a gaseous working fluid from an initial low pressure level to a high pressure level utilizing an available heating medium and utilizing an available cooling medium having a minimum temperature which is above the condensation temperature ofthe low pressure working fluid, which comprises:
(a) absorbing the working fluid being regenerated in an absorption stage by dissolving it in a solvent solution while cooling with such an available cooling medium; the solvent solution comprising a solvent having an initial working
70
75
80
85
90
95
100
105
110
115
120
125
130
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fluid concentration which is sufficient to provide a solvent solution boiling range suitable for absorption ofthe working fluid;
(b) increasing the pressure ofthe solvent solution 5 containing the dissolved working fluid, and evaporating the working fluid being regenerated in an evaporation stage by heating with such an available heating medium;
(c) recovering the evaporated working fluid which 10 is atthe increased pressure level; and
(d) recycling the balance ofthe solvent solution remaining after evaporation ofthe working fluid being regenerated, to constitute the solvent solution forthe absorption stage.
Printed for Her Majesty's Stationery Office by The Tweeddale Press Ltd., Berwick-upon-Tweed, 1982.
Published at the Patent Office, 25 Southampton Buildings, London, WC2A1 AY, from which copies may be obtained.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP19810302177 EP0065042B1 (en) | 1981-05-15 | 1981-05-15 | Generation of energy by means of a working fluid, and regeneration of a working fluid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| GB2098666A true GB2098666A (en) | 1982-11-24 |
Family
ID=8188303
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB8114927A Withdrawn GB2098666A (en) | 1981-05-15 | 1981-05-15 | Generation of energy by means of a working fluid and regeneration of a working fluid |
Country Status (4)
| Country | Link |
|---|---|
| EP (1) | EP0065042B1 (en) |
| DE (1) | DE3173962D1 (en) |
| FR (1) | FR2506386A1 (en) |
| GB (1) | GB2098666A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1991007573A2 (en) * | 1989-11-20 | 1991-05-30 | Vasilios Styliaras | Heat conversion into mechanical work through absorption-desorption |
| GR900100405A (en) * | 1989-11-20 | 1992-04-17 | Vasileios Stuliaras | Meat conversion in mechanic energy |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0160109B1 (en) * | 1980-06-19 | 1989-01-18 | Sonnleitner, Ingolf | Absorption heat pump |
| IL67389A0 (en) * | 1982-12-01 | 1983-05-15 | Gason Energy Eng Ltd | Method and apparatus for the absorption of a gas in a liquid |
| US4503682A (en) * | 1982-07-21 | 1985-03-12 | Synthetic Sink | Low temperature engine system |
| FR2607581B1 (en) * | 1986-12-02 | 1989-01-13 | Ancet Victor | AMBIENT HEAT CONVERTER |
| EP0328103A1 (en) * | 1988-02-12 | 1989-08-16 | Babcock-Hitachi Kabushiki Kaisha | Hybrid rankine cycle system |
| US5029444A (en) * | 1990-08-15 | 1991-07-09 | Kalina Alexander Ifaevich | Method and apparatus for converting low temperature heat to electric power |
| US5440882A (en) * | 1993-11-03 | 1995-08-15 | Exergy, Inc. | Method and apparatus for converting heat from geothermal liquid and geothermal steam to electric power |
| WO2002101206A1 (en) * | 2001-06-12 | 2002-12-19 | Midwest Research Institute | Stratified vapor generator |
| US7305829B2 (en) | 2003-05-09 | 2007-12-11 | Recurrent Engineering, Llc | Method and apparatus for acquiring heat from multiple heat sources |
| US8117844B2 (en) | 2004-05-07 | 2012-02-21 | Recurrent Engineering, Llc | Method and apparatus for acquiring heat from multiple heat sources |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE503537C (en) * | 1927-05-15 | 1930-07-24 | Eduard Fuchs | Power plant powered by ammonia gases |
| GB294882A (en) * | 1927-07-30 | 1929-09-12 | Gen Electric | Improvements in and relating to vapour engines |
| DE2801835A1 (en) * | 1978-01-17 | 1979-07-19 | Dietrich E Dipl Ing Singelmann | Heat engine using absorption process - has two absorbers working at different temp. for greater efficiency |
-
1981
- 1981-05-15 GB GB8114927A patent/GB2098666A/en not_active Withdrawn
- 1981-05-15 DE DE8181302177T patent/DE3173962D1/en not_active Expired
- 1981-05-15 EP EP19810302177 patent/EP0065042B1/en not_active Expired
- 1981-05-21 FR FR8110391A patent/FR2506386A1/en not_active Withdrawn
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1991007573A2 (en) * | 1989-11-20 | 1991-05-30 | Vasilios Styliaras | Heat conversion into mechanical work through absorption-desorption |
| GR900100405A (en) * | 1989-11-20 | 1992-04-17 | Vasileios Stuliaras | Meat conversion in mechanic energy |
| WO1991007573A3 (en) * | 1989-11-20 | 1993-05-13 | Vasilios Styliaras | Heat conversion into mechanical work through absorption-desorption |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0065042B1 (en) | 1986-03-05 |
| DE3173962D1 (en) | 1986-04-10 |
| EP0065042A1 (en) | 1982-11-24 |
| FR2506386A1 (en) | 1982-11-26 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| WAP | Application withdrawn, taken to be withdrawn or refused ** after publication under section 16(1) |